WO2012048217A2 - Procédé pour solidifier des constituants organiques et inorganiques contenus dans de l'eau produite à partir de l'exploitation de pétrole brut - Google Patents

Procédé pour solidifier des constituants organiques et inorganiques contenus dans de l'eau produite à partir de l'exploitation de pétrole brut Download PDF

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Publication number
WO2012048217A2
WO2012048217A2 PCT/US2011/055359 US2011055359W WO2012048217A2 WO 2012048217 A2 WO2012048217 A2 WO 2012048217A2 US 2011055359 W US2011055359 W US 2011055359W WO 2012048217 A2 WO2012048217 A2 WO 2012048217A2
Authority
WO
WIPO (PCT)
Prior art keywords
organic
produced water
oil
water
melt
Prior art date
Application number
PCT/US2011/055359
Other languages
English (en)
Other versions
WO2012048217A3 (fr
Inventor
Keith Minnich
David Gamache
John Kus
Original Assignee
Hpd, Llc
Statoil Canada Ltd.
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Hpd, Llc, Statoil Canada Ltd. filed Critical Hpd, Llc
Priority to CA2813982A priority Critical patent/CA2813982C/fr
Publication of WO2012048217A2 publication Critical patent/WO2012048217A2/fr
Publication of WO2012048217A3 publication Critical patent/WO2012048217A3/fr

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Classifications

    • E—FIXED CONSTRUCTIONS
    • E21—EARTH OR ROCK DRILLING; MINING
    • E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
    • E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
    • E21B43/16—Enhanced recovery methods for obtaining hydrocarbons
    • E21B43/24—Enhanced recovery methods for obtaining hydrocarbons using heat, e.g. steam injection
    • E21B43/2406—Steam assisted gravity drainage [SAGD]
    • E—FIXED CONSTRUCTIONS
    • E21—EARTH OR ROCK DRILLING; MINING
    • E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
    • E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
    • E21B43/34—Arrangements for separating materials produced by the well
    • E21B43/35—Arrangements for separating materials produced by the well specially adapted for separating solids
    • E—FIXED CONSTRUCTIONS
    • E21—EARTH OR ROCK DRILLING; MINING
    • E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
    • E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
    • E21B43/34—Arrangements for separating materials produced by the well
    • E21B43/40—Separation associated with re-injection of separated materials

Definitions

  • the present invention relates to a process for recovering heavy oil and, more particularly, to a process for solidifying inorganic and organic constituents contained in produced water that is a by-product from recovering heavy oil.
  • the present invention relates to a process for concentrating produced water with a high concentration of inorganics and organics which are a byproduct of an oil recovery process.
  • the process includes evaporation of the produced water in a crystallizer which is designed to evaporate virtually all free water from the produced water leaving solid crystals suspended in an organic melt.
  • the organic melt from oil operations is a fluid at temperatures above 100°C. Upon cooling the organics freeze to form a solid. The frozen organic solid traps the suspended solid crystals.
  • the organic solid can be cast in place in a landfill.
  • the present invention entails a method of recovering oil from a SAGD (steam assist gravity drainage) oil well and treating the resulting produced water.
  • SAGD steam assist gravity drainage
  • the terms "oil” and “heavy oil” includes bitumen.
  • This method or process entails recovering an oil-water mixture from an oil well and separating from the oil-water mixture to yield produced water.
  • the produced water is directed to an evaporator that produces a distillate that is directed to a steam generator that produces steam that is injected into an injection well.
  • the evaporator produces a blowdown stream that is directed to a crystallizer.
  • the blowdown is concentrated as water is evaporated from the blowdown.
  • the concentration of the blowdown causes inorganic and organic solids to precipitate from the blowdown and to form an organic melt.
  • the organic melt is cooled to form a solidified structure which is suitable for disposal in a landfill.
  • Figure 1 is a schematic illustration of an exemplary crystallizer used in the process of the present invention.
  • Figure 2 is a schematic representation of a basic process for a heavy oil recovery process according to the present invention.
  • Figure 3 is a schematic illustration of a heavy oil recovery process showing produced water being treated in accordance with the present invention.
  • Figure 4 is a schematic illustration of another heavy oil recovery process showing the blowdown from an evaporator being treated in accordance with the present invention.
  • Enhanced Oil Recovery processes employ thermal methods to improve the recovery of heavy oils from sub-surface reservoirs.
  • the injection of steam into heavy oil bearing formations is a widely practiced enhanced oil recovery method.
  • Steam heats the oil in the reservoir, which reduces the viscosity of the oil and allows the oil to flow to a collection well.
  • Steam condenses and mixes with the oil, the condensed steam being called produced water.
  • the mixture of oil and produced water that flows to the collection well is pumped to the surface. Oil is separated from the produced water by conventional processes employed in conventional oil recovery operations.
  • Another approach is to subject the produced water to an evaporation process to produce distillate which is suitable for steam generation feedwater.
  • the produced water typically contains significant amounts of silica-based compounds, dissolved organics, sparingly soluble salts, and soluble chloride based salts.
  • silica-based compounds, dissolved organics, and sparingly soluble salts will tend to foul process surfaces by deposition of silica on the surfaces, hardness scaling, or organic fouling.
  • These scales and fouling layers reduce the thermal conductivity of heat transfer elements in the evaporator equipment and thus reduce the efficiency of heat exchange and steam generation.
  • the chloride based soluble salts will corrode equipment if allowed to accumulate in the system.
  • the present invention entails a Zero Liquid Discharge (ZLD) process using an ultra high solids crystallizer 10 for heavy oil wastewater treatment wherein inorganic and organic constituents of produced water are converted into a solid for disposal in a landfill.
  • Crystallizer 10 concentrates wastewater with a high fraction of organic solids to a point where virtually all of the free water is removed leaving only solid crystals, such as salt crystals, suspended in an organic melt. Upon cooling the melt solidifies into a material which is suitable for landfill disposal.
  • Fly ash can be added to vary the material handling properties of the melt.
  • Calcium chloride can be added to vary the curing time of the melt.
  • Table 2 shows that the organic matter in these SAGD produced water examples is between 26% and 54% (by weight) of the total solids.
  • produced water from heavy oil recovery processes typically includes several hundred ppms of suspended solids. All of the treatment processes which recycle produced water and generate steam produce concentrated wastewater stream(s). All or a portion of these streams must be purged from the system to prevent accumulation of the dissolved organic and inorganic solids in the system.
  • the present invention is directed, then, at methods of treating the wastewater using a crystallizer, preferably an ultra high solids crystallizer, to produce an organic melt with suspended solid crystals such as salt crystals which will solidify upon cooling into a solid which can be disposed in a landfill.
  • Organic matter is typically long chain hydrocarbon molecules derived from bitumen and dissolved in water.
  • the organics are complex and interact with water in different ways depending on their concentration and temperature. For example, when SAGD produced water is concentrated by evaporation of water to a total solids concentration (defined as the sum of dissolved and suspended organic and inorganic solids) of 50% (by weight) at a temperature of approximately 1 10°C the liquid portion of the mixture has water like properties. When the mixture is cooled to a temperature of 20°C, the suspended solids settle and the remaining liquid has water like properties.
  • Free water is defined as water which is present in liquid form upon cooling of the melt.
  • free water means that when the water cools, it becomes a solid. It should be noted, however, that there is approximately 15-25% water still present in the solidified material. Also it should be noted that free water is water which is easily separated from the melt or for example, would pass through a paint filter if a sample of the solidified melt was set on the filter.
  • Wastewater derived from produced water in the heavy oil recovery process including dissolved inorganic solids, dissolved organic compounds, suspended inorganic and organic solids, and dissolved gases is fed to a crystallizer 10.
  • the total solids concentration in the wastewater typically varies between 10% and 30% by weight.
  • the crystallizer 10 can be fed with more dilute or concentrated wastewater.
  • Crystallizer 10 can be boiler steam driven or use mechanical vapor compression.
  • a recirculation pump 12 draws liquid from a vapor body 14 and pumps the liquid through a heat exchanger 16 and back into the vapor body.
  • Liquid in the vapor body typically has a total solids concentration of approximately 75% (by weight) and a temperature of approximately 1 15°C.
  • Total solids concentration can typically range between 70% and 85% by weight depending on the relative portions of organic and inorganic materials.
  • the temperature can typically vary between approximately 100°C and approximately 120°C when the crystallizer is operated at atmospheric pressure.
  • the heat exchanger 16 includes a steam inlet 16A and a condensate outlet 16B.
  • Water in the recirculating fluid boils off from the fluid in the vapor body 14. These vapors exit the vapor body 14 via a vapor outlet 14A and flow to a condenser in the case of a boiler steam heated system or to a compressor in the case of a mechanical vapor compression system.
  • a portion of the recirculating fluid is discharged via a product outlet 18 as organic melt.
  • Fresh wastewater is introduced via inlet 20 into the recirculating fluid to replace the organic melt which has been discharged and the fluid that has been vaporized.
  • Free water is defined as water which is present in liquid form upon cooling of the melt.
  • the organic melt is a viscous liquid which can be pumped from the crystallizer to a location where it cools into a solid.
  • Fly ash can be blended into the melt so that the blend has properties which make it suitable for solids handling equipment. Blending can be performed using a pug mill, which converts the melt into a semi-solid state. The blend can be discharged from the pug mill onto a conveyer belt for transport to the landfill or discharged into a truck for transport to a landfill. The blend can also be extruded into impermeable casings to prevent contact with water.
  • the ratio of fly ash added to the organic melt is typically in a ratio of 1 to 2 or 1 to 1.
  • the time required for the solidified melt to cure from a semi-solid to a solid can be accelerated by the addition of between 0.5% to 4.0% (by weight) calcium chloride.
  • the concentration of total solids in the crystallizer to reach the no free water condition is typically at least 70% by weight.
  • the material can be encapsulated in various materials or coated with various materials to prevent leaching if the material comes into contact with water.
  • FIG. 2 is a schematic that shows a basic process for treating a produced water stream.
  • produced water is directed to the crystallizer 10 which is preferably a high solids crystallizer.
  • Crystallizer 10 produces a concentrate which contains virtually no free water. Adding fly ash to the concentrate is optional.
  • the concentrate is in the form of an organic melt that contains suspended solid crystals including salt crystals.
  • the organic melt produced by the crystallizer 10 typically forms a viscous semi-solid.
  • the viscous semi-solid is subjected to cooling (Block 30). As discussed above, the cooling causes the organic melt to solidify.
  • the solidified organic melt can be subjected to a coating process (Block 32) and thereafter the solidified organic melt can be disposed of in a landfill.
  • Figures 3 and 4 show two other oil recovery processes that utilize crystallizerl O to produce an organic melt.
  • the organic melt is cooled to form a solidified organic melt having suspended solid crystals contained therein.
  • oil is located or found in an oil bearing formation (Block 40).
  • Various means can be utilized to recovery oil from the oil bearing formation.
  • steam can be injected into an injection well where the steam will ultimately reach the oil and condense to form an oil-water mixture.
  • the oil is removed from the oil bearing formation and brought to the surface in the form of an oil-water mixture (Block 42).
  • the oil-water mixture is directed to an oil-water separator (Block 44).
  • the oil-water separator produces an oil product and produced water.
  • the produced water is directed to an evaporator 52 that produces an evaporator blowdown and a distillate.
  • the evaporator blowdown is directed to the crystallizer 10 which heats the evaporator blowdown and vaporizes liquid therefrom.
  • This concentration process will cause dissolved solids and particularly dissolved salts to precipitate from the concentrated liquid.
  • the precipitants becomes suspended in a hydrocarbon semi-solid melt and during the process these
  • the organic melt is subjected to a cooling process (Block 30).
  • a cooling process (Block 30).
  • Various types of conventional cooling processes can be utilized and as discussed above in one embodiment the organic melt produced by the crystallizer 10 is cooled at a temperature of approximately 20°C to approximately 30°C. This causes the organic melt to become solidified (Block 48).
  • the solidified organic melt with suspended solid crystals therein can then be placed in a landfill.
  • optionally fly ash and/or calcium chloride can be added to the organic melt prior to cooling.
  • Figure 4 is also an oil recovery process and in some respects is similar to the process shown in Figure 3.
  • the Figure 4 process however entails an evaporator 52 that is positioned downstream of the oil-water separator 44.
  • Produced water from the oil-water separator is directed to an evaporator 52 that treats the produced water by producing a distillate (Block 56) and a blowdown (Block 54).
  • the distillate is directed to a steam generator (Block 58).
  • the steam generator 58 can be of various types such as a once-through steam generator followed by a steam-water separator or a package boiler. In either case the steam generator produces steam that is injected into an injection well in the vicinity of the oil bearing formation. The steam ultimately reaches the oil and condenses to form the oil-water mixture that is ultimately pumped to the surface for recovery.
  • the blowdown from the evaporator 52 is directed to the crystallizer 10. More particularly, the blowdown is directed to the vapor body 14 and from the vapor body the blowdown is pumped through the heat exchanger 16 and heated. The heated blowdown including associated vapor is circulated to the vapor body 14. Produced vapor is directed from the vapor body 14 and the concentrated blowdown is continuously recirculated through the pump 12, heat exchanger 16 and vapor body 14. During this process the crystallizer 10 produces the highly concentrated organic melt having the suspended solid crystals contained in the melt. As discussed above the organic melt is cooled to form a solidified organic melt having the suspended solid crystals contained therein which is suitable for disposal in a landfill.
  • the steam generator (Block 58) will produce a blowdown. Blowdown from the steam generator 58 can be recycled to the evaporator feedwater stream. Further, regeneration waste from various components of the system shown in Figure 4 can be directed to the crystallizer 10 for further treatment.
  • the percentage compositions are always by weight.

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  • Geology (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Mining & Mineral Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Fluid Mechanics (AREA)
  • Physics & Mathematics (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Geochemistry & Mineralogy (AREA)
  • Processing Of Solid Wastes (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Heat Treatment Of Water, Waste Water Or Sewage (AREA)
  • Fats And Perfumes (AREA)

Abstract

L'invention concerne un procédé de traitement de l'eau produite récupérée à partir d'un processus de récupération assistée du pétrole. Un mélange d'huile-eau est recueilli à partir d'une formation pétrolifère. Le mélange d'huile-eau est dirigé vers un séparateur qui sépare le mélange d'huile-eau pour donner de l'eau produite et un produit d'huile. L'eau produite inclut de l'eau, des solides organiques dissous et des solides inorganiques dissous. L'eau produite est dirigée vers un cristalliseur. Dans le cristalliseur, l'eau produite est concentrée par chauffage de l'eau produite. La concentration de l'eau produite provoque la précipitation des solides organiques et inorganiques à partir de l'eau produite et la formation des cristaux solides, dont des cristaux de sel. De plus, la concentration de l'eau produite dans le cristalliseur produit une masse fondue organique incluant des cristaux solides. Après quoi, le processus ou le procédé comporte le refroidissement de la masse fondue organique de telle sorte que la masse fondue organique se solidifie en une structure solide organique, et où pratiquement aucune eau libre n'est présente dans la structure solide organique.
PCT/US2011/055359 2010-10-08 2011-10-07 Procédé pour solidifier des constituants organiques et inorganiques contenus dans de l'eau produite à partir de l'exploitation de pétrole brut WO2012048217A2 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CA2813982A CA2813982C (fr) 2010-10-08 2011-10-07 Procede pour solidifier des constituants organiques et inorganiques contenus dans de l'eau produite a partir de l'exploitation de petrole brut

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US39120510P 2010-10-08 2010-10-08
US61/391,205 2010-10-08

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WO2012048217A2 true WO2012048217A2 (fr) 2012-04-12
WO2012048217A3 WO2012048217A3 (fr) 2012-06-21

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US (1) US8506467B2 (fr)
CA (1) CA2813982C (fr)
WO (1) WO2012048217A2 (fr)

Families Citing this family (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20130075333A1 (en) 2011-09-22 2013-03-28 Randall B. Pruet Apparatus and Process for Treatment of Water
US9243482B2 (en) * 2011-11-01 2016-01-26 Nem Energy B.V. Steam supply for enhanced oil recovery
US9738553B2 (en) 2012-03-16 2017-08-22 Aquatech International, Llc Process for purification of produced water
CA2794356C (fr) * 2012-09-13 2018-10-23 General Electric Company Traitement d'eau produite avec un evaporateur a culture
CA2789822C (fr) 2012-09-13 2019-06-04 General Electric Company Traitement d'eau produite et precipitations solides issues de vidange de traitement thermique
CA2789820C (fr) 2012-09-13 2019-11-26 General Electric Company Traitement de concentre d'eau produite
CA2860275C (fr) 2014-06-02 2016-10-25 Veolia Water Solutions & Technologies North America, Inc. Procede de recuperation d'hydrocarbure incluant un cristalliseur de solides destine au traitement de vidange d'evaporateur
EP3465001B1 (fr) * 2016-06-03 2023-01-11 Sowers, Hank James Système et procédé de traitement de l'eau
US20180050944A1 (en) * 2016-08-16 2018-02-22 Naveed Aslam Methods for reclaiming produced water

Citations (4)

* Cited by examiner, † Cited by third party
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US3230282A (en) * 1961-11-13 1966-01-18 Shell Oil Co Process and apparatus for separating materials
US5028336A (en) * 1989-03-03 1991-07-02 Texaco Inc. Separation of water-soluble organic electrolytes
US20070102154A1 (en) * 1998-07-06 2007-05-10 Grott Gerald J Mothods of utilizing waste wasters produced by water purification processing
US20100038081A1 (en) * 2008-08-18 2010-02-18 Hpd, Llc Method for removing silica from evaporator concentrate

Family Cites Families (3)

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Publication number Priority date Publication date Assignee Title
US7077201B2 (en) * 1999-05-07 2006-07-18 Ge Ionics, Inc. Water treatment method for heavy oil production
US7959012B2 (en) * 2005-05-19 2011-06-14 M-I L.L.C. Oil-based sludge separation and treatment system
US8127843B2 (en) * 2006-03-24 2012-03-06 Ge Ionics, Inc. Solidification of residuals from water treatment systems in heavy oil recovery operations

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3230282A (en) * 1961-11-13 1966-01-18 Shell Oil Co Process and apparatus for separating materials
US5028336A (en) * 1989-03-03 1991-07-02 Texaco Inc. Separation of water-soluble organic electrolytes
US20070102154A1 (en) * 1998-07-06 2007-05-10 Grott Gerald J Mothods of utilizing waste wasters produced by water purification processing
US20100038081A1 (en) * 2008-08-18 2010-02-18 Hpd, Llc Method for removing silica from evaporator concentrate

Also Published As

Publication number Publication date
CA2813982C (fr) 2014-02-11
US8506467B2 (en) 2013-08-13
US20120087737A1 (en) 2012-04-12
WO2012048217A3 (fr) 2012-06-21
CA2813982A1 (fr) 2012-04-12

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